Process for hydrogenation of chlorosilane

Abstract: A process for the hydrogenation of chlorosilanes comprising contacting a chlorosilane with aluminum and a hydrogen source selected from hydrogen gas and gaseous hydrogen chloride in the presence of a catalyst. The catalyst is selected from copper and copper compounds, tin and tin compounds, zinc and zinc compounds and mixtures thereof.

Description: The present invention is a process for the hydrogenation of chlorosilanes. The process comprises contacting a chlorosilane with aluminum and a hydrogen source selected from hydrogen gas and gaseous hydrogen chloride in the presence of a catalyst. The catalyst is selected from copper compounds, tin and tin compounds, zinc and zinc compounds and mixtures thereof. Industrially significant methods for producing hydrosilanes involve the reaction of a halosilane with a metal hydride in the presence of a solvent as described in Kirk and Othmer, Encyclopedia of Chemical Technology; The Interscience Group, New York, N.Y, Vol. 12, p. 368, 1978. The preferred metal hydride reagents are LiAlH 4 and NaAlH 4 . The reaction is reported to proceed quantatively at low system pressure and temperature. However, metal hydride reagents offer significant processing disadvantages. First, they are highly reactive and may oxidize exothermically to release explosive concentrations of hydrogen gas. Because of this, hydrogenation reactions with these reagents are typically carried out in solvents. The use of solvents presents a second disadvantage in that the solvent must be separated from the product. If solvents are not used, the metal may be stabilized by replacing a portion of the metal hydride ligands with bulky organic substituents. While this eliminates the solvent, it necessarily reduces the equivalent hydrogenation potential for the metal hydrides. Non-metal hydride, non-solvent systems for hydrogenating halosilanes have been reported. US-A-2,406,605 disclosed the reaction of halosilanes with hydrogen or a hydrogen halide at an elevated temperature with a metal selected from aluminum, magnesium and zinc. At temperatures of 400°C. to 500°C. and atmospheric pressure, SiCl 4 and MeSiCl 3 were reacted to SiHCl 3 and MeHSiCl 2 respectively. However, the reaction of Me 2 SiCl 2 was generally unsuccessful, even at 500°C. US-A-2,458,703 reported a method of hydrogenating halosilanes using silicon as a chloride acceptor in a continuous high-pressure system. It reported that the silicon could reduce a halosilane in a hydrogen atmosphere when AlCl 3 or AlBr 3 was present. US-A-2,595,620 found that silicon could be used to reduce a chlorosilane with hydrogen at temperatures above 400°C. and that AlCl 3 or AlBr 3 was not necessary. US-A-3,057,686 described a hydrogenation process where a halosilane was reacted with hydrogen and activated aluminum metal at superatmospheric pressure. The activated aluminum was a metal having an essentially oxygen free surface. The groups of compositions suitable for activating the aluminum were (1) metal hydrides, (2) mixtures of iodine and an alkyl halide in which the halogen has an atomic number of at least 17 and (3) trialkyl aluminum compounds. US-A-3,100,788 claimed a process for hydrogenation of halosilanes with hydrogen gas using sodium metal as the halogen receptor. GB 609 134 A discloses a method of replacing at least some of the halogen atoms in a halogenated silane with hydrogen which consists in contacting a mixture of the halogenated silane and a material selected from the class consisting of hydrogen and hydrogen halides in the vapor state and at an elevated temperature with a metal selected from the class consisting of aluminum, magnesium and zinc. In example 2 of said document methyltrichlorosilane and hydrogen gas are passed over a mixture of aluminum granules and copper metal powder. EP 0 365 207 A discloses a process for the preparation of more highly alkylated silanes comprising (A) contacting a halide of silicon with an alkyl halide in the presence of a metal such as aluminum, which serves as a halogen acceptor and a sufficient quantity of a catalyst effective in improving exchange of the alkyl groups from the alkyl halide with said halogen atoms of said halide of silicon; (B) reacting the halide of silicon with the alkyl halide in the presence of the metal and the catalyst at a temperature greater than about 150 °C to form the more highly alkylated silanes and a metal halide; and (C) isolating and separating the more highly alkylated silanes. The present invention is a process for the hydrogenation of chlorosilane by a hydrogen source selected from hydrogen gas and gaseous hydrogen chloride. Our process uses aluminum as the halogen receptor and it does not require a solvent and/or super-atmospheric pressure. Our process also requires a catalyst selected from a group consisting of copper compounds, tin and tin compounds, zinc and zinc compounds and mixtures thereof. Under these process conditions, the catalyst provides for increased formation of silicon hydrogen bonds and increased chlorosilane conversion, when compared to the use of aluminum without a catalyst. The catalyst also allows the process to be run at a lower temperature than that used for similar uncatalyzed processes. Hydrosilanes prepared by the present process are useful intermediates in the formation of silicone polymers, elastomers and resins. The present invention is a process for the hydrogenation of chlorosilanes. The process comprises contacting a chlorosilane described by formula R a H b SiCl 4-a-b where each R is independently selected from alkyls comprising one to six carbon atoms, a=0, 1, 2 or 3; b=0, 1, 2 or 3; and a+b=0, 1, 2 or 3; with aluminum and a hydrogen source selected from hydrogen gas or gaseous hydrogen chloride, in the presence of a catalyst selected from copper compounds, tin and tin compounds, zinc and zinc compounds and mixtures thereof and recovering a hydrosilane resulting from the exchange of one or more of the chlorine atoms of the chlorosilane by hydrogen. Contacting the chlorosilane with aluminum, hydrogen source and catalyst can be effected in standard reactors for contacting chlorosilanes and solids. The reactor can be a fixed-bed reactor, a stirred-bed reactor or a fluidized-bed reactor. The present process can be run as a batch process, semi-continuous or continuous process. Since the aluminum trichloride produced in the present process can act as a redistribution catalyst for alkyls and hydrogen substituted on silicon, it is generally preferred that the process be run as a continuous process in a fluidized bed reactor or a packed bed reactor to allow rapid separation of the aluminum trichloride from the hydrogenated chlorosilanes. Chlorosilanes which can be hydrogenated in the present process are described by formula (1). In formula (1) each R is independently selected from alkyls comprising one to six carbon atoms. The alkyl can be methyl, ethyl, propyl, isopropyl, n-butyl, tert-butyl and hexyl. Preferred is when R is methyl. Chlorosilanes which can be hydrogenated by the present invention include tetrachlorosilane, methyltrichlorosilane, dimethyldichlorosilane and trimethylchlorosilane. The present process is especially useful for hydrogenating dimethyldichlorosilane to dimethylchlorosilane. The present process employs aluminum as a chlorine receptor, forming aluminum chloride as a by-product. The aluminum can be added to the process as a powder, particulate, flakes, shot or wire. Typically, the present process is run using a fixed-bed or fluidized-bed of aluminum. Therefore, the process is run using a large excess of aluminum in relation to that required as a chlorine receptor. The present process uses a catalyst selected from copper compounds, tin and tin compounds, zinc and zinc compounds and mixtures thereof. The catalyst can be of the same physical forms as described for the aluminum. It is preferred, but not necessary, that the catalyst be mixed with the aluminum to form a relatively homogeneous mixture. Mixing can be accomplished by standard means for mixing powders, for example, mechanical stirring or shaking. The catalyst can be copper compound or a mixture thereof. The copper compound can be an inorganic or organic compound of copper. The inorganic copper compound can be a copper halide or copper oxide. A preferred organic copper compound is copper formate. The copper compound or a mixture thereof is added to the process to provide a concentration of copper of 0.1 to 20 weight percent in relation to the aluminum. The catalyst can be tin metal, tin compound or a mixture thereof. The catalyst can be an inorganic or organic tin compound. The inorganic tin compound can be, for example, tin halide or tin hydride. The inorganic tin compound is preferably tin chloride. The catalyst can also be an organic tin compound such as trimethyltin. The weight of tin, tin compound or mixture thereof used as a catalyst in the present process must provide 1500 ppm to 10,000 ppm tin in relation to the weight of the aluminum. Preferred is when the weight of tin provided to the process as catalyst is within a range of 3,000 ppm to 5,000 ppm. The catalyst can be zinc metal, a zinc compound or a mixture thereof. The catalyst can be an inorganic zinc compound or an organic zinc compound. The inorganic zinc compound can be a zinc halide or zinc hydride. The organic zinc compound can be dimethylzinc. All or a portion of the zinc may be provided to the process by brass. The weight of zinc, zinc compound or mixture thereof used as a catalyst in the present process must provide 100 ppm to 10,000 ppm zinc in relation to the weight of the aluminum. The catalyst can be a mixture comprising one or more of copper compounds, tin metal, tin compounds, zinc metal and zinc compounds. A preferred catalyst for the present process is a mixture comprising CuCl, tin metal and zinc metal. It is desirable that this mixture be added to the process to provide a final concentration with relation to the weight of the aluminum of 0.1 to 20 percent CuCl, 5 to 2000 ppm tin and 100 to 10,000 ppm zinc. All or a portion of the zinc in the catalyst mixture may be provided by brass. A preferred catalyst mixture provides in mixture with the aluminum about 10-15 weight percent CuCl, 1500-2000 ppm tin and 3500-4200 ppm brass. The present process employs a hydrogen source to reduce the chlorosilane. The hydrogen source is selected from hydrogen gas or gaseous hydrogen chloride. For optimal results, it is preferred that the mole ratio of hydrogen source provide at least one mole of hydrogen per mole of chlorosilane. A lesser mole ratio of hydrogen to chlorosilane may be used, but it may also result in reduced process yield. It is preferred that the mole ratio of hydrogen to chlorosilane (H:Si) be within a range of one to four. Generally, increasing the mole ratio of hydrogen increases the average number of hydrogens atoms bonded to the silicon of the chlorosilane. The present process can be run at a reactor pressure of 0.1 to 10.1 MPa (one atmosphere (atm) to 100 atm). It is preferred that the process be run at a reactor pressure within a range of 0.1 to 1.5 MPa (one atm to fifteen atm). Residence time of the chlorosilane within the reactor general requires a balancing between allowing sufficient time for hydrogenation to occur without excessive redistribution of silicon-bonded alkyl substituents. Generally a residence time of 0.1 second to 5 minutes is useful. Preferred is a residence time of one second to one minute. The preferred temperature for running the present process will depend upon the chlorosilane and the hydrogen source fed to the process. Generally, as the temperature is increased the conversion of feed chlorosilanes to other species increases, but the redistribution reaction of silicon-bonded alkyls also increases. When the hydrogen source is hydrogen gas, a useful temperature range is within a range of 300°C. to 450°C. When the hydrogen source is hydrogen gas, a preferred temperature is within a range of 325°C. to 375°C. When the hydrogen source is gaseous hydrogen chloride, a useful temperature is within a range of 250°C. to 450°C. When the hydrogen source is gaseous hydrogen chloride, a preferred temperature is within a range of 270°C. to 350°C. We have also found that the present process is more consistent in product distribution and yield when the mixture comprising the aluminum and catalyst is preheated prior to contact with the chlorosilane and hydrogen source. Therefore, in a preferred embodiment the mixture comprising aluminum and the catalyst is preheated. Preheating can be conducted at any temperature within the temperature ranges provided for conduct of the process. The length of time of preheating will depend both upon the efficiency of heating and should be determined for each specific reactor configuration. For example, using a reactor described in the present examples, an optimal heating time was found to be within a range of eight to 13 minutes. However, preheating times of 0.5 minute to 45 minutes were found to be useful. In the present process one or more of the chlorine atoms substituted on the silicon atoms of the chlorosilane is replaced with hydrogen forming a hydrosilane product. The hydrosilane product can be dimethylsilane, dimethylchlorosilane, methyldichlorosilane and trimethylsilane. A preferred hydrosilane product is selected from dimethylchlorosilane or trimethylsilane. The following examples are provided to illustrate the present invention. Example 1 (Control) The hydrogenation of dimethyldichlorosilane by hydrogen gas in the presence of aluminum, with no catalyst, was evaluated. The process was conducted in a 25.4 mm (one-inch) carbon-steel reactor which was immersed in a fluidized-sand temperature bath. The input end of the reactor was connected to a stainless steel vaporization coil which was also immersed in the temperature bath and which served to vaporize the dimethyldichlorosilane. The reactor exit was connected to a series of two flasks serving as collection traps. The first trap was maintained at a temperature of 100°C. to trap aluminum trichloride exiting the reactor. The second trap was immersed in dry ice and served to collect the chlorosilanes exiting the reactor. The reactor was charged with 90 g of powdered aluminum (Alcan 44™, Alcan-Toyo American, Joliet, IL). The reactor was purged with nitrogen gas and placed into the temperature bath maintained at a temperature of 365°C. The reactor was allowed to set in the temperature bath for 12 minutes as a preheat treatment. Then, hydrogen gas and dimethyldichlorosilane were fed to the reactor at a molar ratio of hydrogen to chlorosilane (H:Si) of 2.3 with a residence time in the reactor of 11 seconds. Pressure in the reactor was 101.3 kPa (one atm). Feed to the reactor was continued for five hours, with gases exiting the reactor being collected in the described traps. The collected chlorosilane was analyzed by gas chromatography (GC) using a thermoconductivity detector (TC). A mass spectrometer (MS) was periodically used to confirm composition. The results are reported in Table 1. The heading "%Si Conv." represents the percent conversion of the dimethyldichlorosilane to other species. Reaction of Dimethyldichlorosilane With Hydrogen Gas and Aluminum in The Absence of Catalyst Weight Percent Product Distribution % Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 0.4 0.0 68.0 15.2 0.0 0.0 0.0 16.8 0.0 In Tables 1-9b, Me 2 H 2 = Me 2 SiH 2 , Me 2 H = Me 2 HSiCl 2 , MeH = MeHSiCl 2 , Me 3 H = Me 3 SiH, Me = MeSiCl 3 , Me 2 = Me 2 SiCl 2 , Me 3 = Me 3 SiCl and Me 4 = Me 4 Si. Example 2 A series of runs was conducted to evaluate the variability of the process when no preheating of a mixture of tin catalyst and aluminum is used prior to contacting with a mixture of dimethyldichlorosilane and hydrogen gas. The runs were conducted in a reactor similar to that described in Example 1. Powdered tin (Belmont Metals Inc., Brooklyn, NY) was mixed with 90 g of aluminum (as previously described) at a concentration of 4000 ppm. This mixture was added to the reactor and the reactor purged with nitrogen. The reactor was immersed in a temperature bath at 365°C. and the feed of dimethyldichlorosilane and hydrogen gas immediately started to the reactor. The molar ratio of hydrogen to dimethyldichlorosilane was within a range of 2.9 to 3.2. Residence time of the reactants within the reactor was 12 to 13 seconds. All runs were conducted at a reactor pressure of 101.3 kPa (one atm). Products from each run were collected and analyzed as described in Example 1. The results are reported in Table 2. Tin Catalyzed Reaction of Dimethyldichlorosilane With Hydrogen Gas and Aluminum - No Preheat Treatment Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 137 8.0 0.5 16.4 0.6 0.0 1.0 0.0 80.2 1.2 140 50.6 1.0 10.7 0.1 0.7 0.0 0.0 84.4 3.1 141 59.1 0.2 8.5 0.3 0.6 0.0 0.0 87.6 2.8 For the data provided in Table 2, the average value for % Si Conv. is 39.2. Example 3 A series of runs was conducted to evaluate the variability of the process when a mixture of aluminum and tin is subject to a preheat treatment prior to contact with a dimethyldichlorosilane and hydrogen gas mixture. The runs were conducted in a reactor similar to that described in Example 1. A mixture of tin and aluminum as described in Example 2 was formed and added to the reactor. The reactor was purged with nitrogen, placed in a 365°C. temperature bath for eight to 13 minutes and then feed of a mixture of dimethyldichlorosilane and hydrogen gas was started. The molar ratio of hydrogen to dimethyldichlorosilane was within a range of 3.1 to 3.4. Residence time of the reactants within the reactor was 12 to 13 seconds. For all runs, the pressure in the reactor was 101.3 kPa (one atm). Products from each run were collected and analyzed as described in Example 1. The results are reported in Table 3. Tin Catalyzed Reaction of Dimethyldichlorosilane With Hydrogen Gas and Aluminum - Effects of Heat Pretreatment Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 144 59.4 1.0 7.3 0.3 3.1 0.2 0.0 84.2 4.0 145 66.2 0.6 5.8 0.3 0.4 0.2 0.0 90.0 2.8 148 42.1 0.1 11.3 0.8 0.4 0.1 0.0 86.8 0.6 149 82.0 0.4 4.9 0.2 1.6 1.5 0.0 88.8 2.5 For the data provided in Table 3, the average value for % Si Conv. is 62.5. Example 4 The ability of tin to catalyze the reaction of dimethyldichlorosilane with hydrogen gas and aluminum was evaluated at a temperature of 325°C. Two runs were made in a reactor similar to that described in Example 1. A mixture of aluminum and tin as described in Example 2 was formed and added to the reactor. The reactor was purged with nitrogen and placed in a 325°C. temperature bath for 10 minutes before start of the dimethyldichlorosilane and hydrogen gas feed. The molar ratio of hydrogen to dimethyldichlorosilane was 3.0 to 3.1. Residence time of the reactants within the reactor was 5.3 to 5.8 seconds. Pressure in the reactor was 101.3 kPa (one atm). Products from each run were collected and analyzed as described in Example 1. The results are reported in Table 4. Tin Catalyzed Reaction of Dimethyldichlorosilane With Hydrogen Gas and Aluminum at 325°C. Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 242 1.3 0.0 12.8 0.0 2.2 0.0 0.0 73.0 12.1 243 1.1 0.0 16.2 0.0 0.9 0.0 0.0 68.6 14.3 Example 5 The tin catalyzed reaction of methyltrichlorosilane with hydrogen gas and aluminum was evaluated at 101.3 kPa (one atmosphere) of pressure and at 405.2 kPa (four atmospheres) of pressure. The runs were conducted in a reactor similar to that described in Example 1. Mixtures of tin and aluminum as described in Example 2 were formed and added to the reactor. The reactor was purged with nitrogen and pre-heated in a 365°C. temperature bath for 11 to 12 minutes prior to start of a methyltrichlorosilane and hydrogen gas feed to the reactor. For run number 156, the pressure within the reactor was 101.3 kPa (one atm). The molar ratio of hydrogen to methyltrichlorosilane was 1.15 and the residence time of the reactants within the reactor was 10.4 seconds. For run number 153, the pressure in the reactor was 405.2 kPa (four atmospheres). The molar ratio of hydrogen to methyltrichlorosilane was 2.9 and the residence time of the reactants within the reactor was 52.2 seconds. Products from the reactor were collected and analyzed as described in Example 1. The results are reported in Table 5. Tin Catalyzed Reaction of Methyltrichlorosilane With Hydrogen Gas and Aluminum Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 156 0.1 0.0 4.0 50.0 0.0 0.0 0.0 40.0 4.0 153 4.4 0.3 0.9 30.4 0.0 0.0 52.6 15.9 0.0 Example 6 The tin catalyzed reaction of trimethylchlorosilane with hydrogen gas and aluminum was evaluated. The run was conducted in a reactor similar to that described in Example 1. A mixture of tin and aluminum as described in Example 2 was formed and added to the reactor. The reactor was purged with nitrogen, placed in a 400°C. temperature bath and feed started to the reactor immediately. The molar ratio of hydrogen to trimethylchlorosilane was 2.8. Residence time of the reactants within the reactor was 12.5 seconds. Product from the reactor was collected and analyzed as described in Example 1. The results are reported in Table 6. Tin Catalyzed Reaction of Trimethylchlorosilane With Hydrogen Gas and Aluminum Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 139 79.6 2.2 0.5 0.2 17.8 0.3 0.2 0.0 78.9 Example 7 The tin catalyzed reaction of dimethyldichlorosilane with hydrogen gas and aluminum was evaluated at a reactor pressure of 405.2 kPa (four atmospheres). The run was conducted in a reactor similar to that described in Example 1. A mixture of tin and aluminum as described in Example 2 was formed and added to the reactor. The reactor was purged with nitrogen and preheated in a 365°C. temperature bath for nine minutes prior to start of feed of a dimethyldichlorosilane and hydrogen gas mixture. The molar feed ratio of hydrogen to dimethyldichlorosilane was 1.8 and the residence time was 49.8 seconds. Product from the reactor was collected and analyzed as described in Example 1. The results are reported in Table 7. Tin Catalyzed Reaction of Dimethyldichlorosilane With Hydrogen Gas and Aluminum at 405.2 kPa (Four Atmospheres) Pressure Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 161 87.0 3.8 4.0 0.0 13.4 0.1 0.0 49.3 29.3 Example 8 Two runs were conducted to evaluate the ability of a catalyst mixture comprising cuprous chloride, tin and brass to catalyze the reaction of dimethyldichlorosilane with hydrogen gas and aluminum. The runs were conducted in a reactor similar to that described in Example 1. 90 g of an aluminum and catalyst mixture comprising 12 weight percent CuCl, 1800 ppm tin and 3900 ppm brass was used in each run. The reactor was purged with nitrogen and preheated at the reaction temperature for 10 to 12 minutes. Run number 244 was conducted at a bath temperature of 325°C. For Run number 244, the molar feed ratio of hydrogen to dimethyldichlorosilane was 3.3 and the residence time of the reactants within the reactor was 5.3 seconds. The reactor pressure was 101.3 kPa (one atm). Run number 251 was conducted at a bath temperature of 365°C. For Run number 251, the molar feed ratio of hydrogen to dimethyldichlorosilane was 3.6 and the residence time of the reactants within the reactor of 5.2 seconds. The reactor pressure was 101.3 kPa (one atm). Product from each run was collected and analyzed as described in Example 1. The results are reported in Table 8. Catalytic Effect of Mixture Comprising Cuprous Chloride, Tin and Brass on Reaction on Reaction of Dimethyldichlorosilane With Hydrogen Gas and Aluminum Weight Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 244 65.8 0.26 16.6 0.0 0.5 0.0 0.0 82.1 0.6 251 80.2 1.37 16.7 0.0 1.9 0.9 0.0 76.8 1.8 Example 9 A series of runs was conducted to evaluate the tin catalyzed reaction of dimethyldichlorosilane with gaseous hydrogen chloride and aluminum. The runs were conducted in a reactor similar to that described in Example 1. A mixture of tin and aluminum as described in Example 2 was formed and added to the reactor. The reactor was purged with nitrogen and placed in the temperature bath. Table 9a presents, for each run, the molar ratio of hydrogen chloride to dimethyldichlorosilane (H/Si), the residence time (Res., s), temperature of the temperature bath (Bath Temp., oC), pressure within the reactor (Press., atm.) and the time of preheating of the catalyst and aluminum mixture (Preheat, Min.) In all cases where the catalyst and aluminum mixture were preheated, the preheating temperature was that at which the reaction was conducted. Process Parameters Run No. H/Si Res. (s) Bath Temp. (°C.) Press. (kPa) Pre-Heat (Min.) 126 0.94 8.97 262 101.3 0 128 3.13 4.56 240 101.3 0 168 1.52 9.54 300 101.3 10 170 3.18 7.65 365 101.3 8 For each run, product from the reactor was collected and analyzed as described in Example 1. The results are reported in Table 9 Tin Catalyzed Reaction of Dimethyldichlorisilane With Hydrogen Chloride Gas and Aluminum Mole Percent Product Distribution Run No. %Si Conv. Me 2 H 2 Me 2 H MeH Me 3 H Me Me 2 Me 3 Me 4 126 5.2 0.0 24.7 29.9 0.0 11.3 0.0 29.9 0.1 128 8.0 0.0 34.1 2.4 0.0 30.6 0.0 27.4 0.1 168 7.4 0.0 31.1 0.0 0.0 14.3 0.0 54.6 0.1 170 96.4 2.2 1.6 0.0 9.1 0.9 0.0 60.3 21.3

Claims: A process for the hydrogenation of chlorosilanes, the process comprising contacting a chlorosilane described by formula R a H b SiCl 4-a-b , where each R is independently selected from alkyls comprising one to six carbon atoms, a=0, 1, 2 or 3; b=0, 1, 2 or 3; and a+b=0, 1, 2 or 3; with aluminum and a hydrogen source selected from hydrogen gas or gaseous hydrogen chloride in the presence of a catalyst selected from copper compounds, tin and tin compounds, zinc and zinc compounds and mixtures thereof and recovering a hydrosilane resulting from the exchange of one or more of the chlorine atoms of the chlorosilane by hydrogen. The process according to claim 1 where the process is run as a continuous process in a fluidized-bed reactor or a packed-bed reactor. The process according to claim 1 where the catalyst comprises copper at a concentration of 0.1 to 20 weight percent relative to the aluminum. The process according to claim 1 where the catalyst comprises tin at a concentration of 1500 ppm to 10,000 ppm relative to the aluminum. The process according to claim 1 where the catalyst comprises zinc at a concentration of 100 ppm to 10,000 ppm relative to the aluminum. The process according to claim 1 where a mixture comprising CuCl, tin metal and zinc metal is added to the process to provide a concentration relative to the aluminum of 0.1 to 20 weight percent CuCl, 5 to 2000 ppm tin and 100 to 10,000 ppm zinc. The process according to claim 1 where the hydrogen source provides at least one mole of hydrogen per mole of chlorosilane. The process according to claim 1 where the process is conducted at a pressure of 0.1 to 10.1 MPa (one atm to 100 atm). The process according to claim 1 where the process is conducted at a temperature within a range of 250°C. to 450°C, if the hydrogen source is hydrogen chloride, and at a temperature within a range of 300°C to 450°C, if the hydrogen source is hydrogen gas. The process according to claim 1 where a mixture comprising the aluminum and the catalyst is preheated. The process according to claim 1 where the hydrosilane is dimethylchlorosilane or trimethylsilane.

Inventors: CHADWICK KIRK MICHAEL, HALM ROLAND LEE, KEYES BRIAN ROBERT, CHADWICK, KIRK MICHAEL, HALM, ROLAND LEE, KEYES, BRIAN ROBERT
Applicants: DOW CORNING, DOW CORNING CORPORATION
Application year: 1994
Main classification: C07F7
IPC codes: C07F7, C07B61, B01J23, C01B33, B01J27